Syngas biomethanation process and anaerobic digestion system

ABSTRACT

An anaerobic digester is fed a feedstock, for example sludge from a municipal wastewater treatment plant, and produces a digestate. The digestate is dewatered into a cake. The cake may be dried further, for example in a thermal drier. The cake is treated in a pyrolysis system to produce a synthesis gas and biochar. The gas is sent to the same or another digester to increase its methane production. The char may be used as a soil enhancer.

CROSS-REFERENCES TO RELATED APPLICATIONS

This application is a continuation-in-part of PCT/CA2013/050037 filed onJan. 21, 2013, which claims the benefit of priority from U.S.Provisional Application Nos. 61/589,663 filed on Jan. 23, 2012 and61/652,260 filed on May 28, 2012. PCT/CA2013/050037 filed on Jan. 21,2013 and U.S. Provisional Application Nos. 61/589,663 filed on Jan. 23,2012 and 61/652,260 filed on May 28, 2012 are incorporated by reference.

FIELD

This specification relates to wastewater treatment, anaerobic digestion,pyrolysis and gasification.

BACKGROUND

The following discussion is not an admission that anything discussedbelow is common general knowledge or citable as prior art.

Anaerobic digestion produces biogas as a result of the biologicalfermentation of volatile solids (VS) supplied with the feedstock. Thedegree of volatile solids reduction is related to the biodegradabilityof the feedstock and process conditions in the digester. Importantdigester parameters or considerations include temperature, pH,food-to-microorganism ratio, organic loading rate, hydraulic and solidsretention time, absence of toxic substances at inhibitoryconcentrations, adequate mixing, and others. The closer these conditionsare to an optimum, the higher the VS reduction will be.

Typically, digesters treating complex organic substrates will achieve 60to 80% VS reduction. With substrates with high fiber content, such assilage or dairy manure, a digester may achieve about 60% VS destruction.Typical digesters treating municipal sewage sludge produced in awastewater treatment plant usually achieve about 50% VS destruction in20 day hydraulic retention time (HRT) mesophilic digesters.

The digester sludge, or digestate, produced by an anaerobic digester isa combination of inert solids that were fed with the substrate,recalcitrant volatile solids that could not be degraded biologically,and bacterial biomass that grew as a result of feeding on the degradableportion of the volatile solids fed with the feedstock. A typicaldigestate solids content is 2% to 10% total solids (TS) or dried solids(DS), depending on the substrate and the type of digester. The digestatemay be dewatered mechanically to produce a cake with 20 to 30% solids,depending among other things on the undigested fiber content and thetype of dewatering device used.

Pyrolysis is a technique typically used to process solid waste such aswood chips or sawdust. Pyrolysis produces biochar, liquids and gasesfrom a biomass by heating the biomass in a low or no oxygen environment.The absence or deficiency of oxygen prevents combustion. The relativeyield of products from pyrolysis varies with temperature. Temperaturesof 400-500° C. (752-932° F.) produce more char, while highertemperatures, up to and above 700° C. (1,292° F.) favor the yield ofliquid and gas fuel components. Pyrolysis occurs more quickly at thehigher temperatures, typically requiring seconds instead of hours. Hightemperature pyrolysis is also known as gasification, and producesprimarily synthesis gas. Once initiated, both processes can be selfsupporting and produce net energy, not accounting for the energy valueof the biomass consumed.

Synthesis gas, also called syngas or producer gas, is a combination ofCO, H₂ and CO₂ that results from the thermal degradation of biomasswithout combustion, through pyrolysis or gasification. This processoccurs typically at temperatures between 500 and 700 deg C. with minimalintroduction of oxygen, if any. Other components of syngas are watervapor, methane, light hydrocarbons, particulates and volatileimpurities. Syngas has a low heat value, for example 120 to 150Btu/cubic foot. After adequate cleaning to remove moisture,particulates, tars and impurities, syngas can be used for heat orelectricity production with adapted internal combustion engines,boilers, gas turbines, or fuel cells. In some gasification systems,syngas is subject to high temperature steam reformation to producehydrogen that is either sold as a gaseous fuel or used on site to powerfuel cells.

In some cases, syngas is upgraded to methane with chemical catalysts. Inone process, a water-gas shift (WGS) step increases the H₂/CO ratio ofthe syngas and is followed by a nickel catalyst supported step thatenables conversion from CO and CO₂ into methane and water. This processis costly due to the chemical catalyst, its energy demand, and the needto pre-treat the syngas to remove impurities.

INTRODUCTION TO THE INVENTION

The following introduction is intended to introduce the reader to thedetailed description and claims to follow, but is not intended to limitor define the claims.

The solids in digestate have an energy content resulting from theirpotential to be oxidized. This energy content can be extracted bypyrolysis or gasification of the digestate to produce syngas, optionallyafter further drying or dewatering. The syngas can be converted to abiogas containing mostly methane by anaerobic microorganisms.

In a process and apparatus described herein, syngas is added into ananaerobic digester to produce methane. The syngas can come frompyrolysis or gasification of a raw biomass such as wood, municipalsolids waste, municipal yard waste, waste activated sludge frommunicipal sewage treatment, agricultural residues, etc., or frompyrolysis or gasification of a dewatered and optionally partially drieddigestate cake produced by the same or another digester at the same oranother digestion facility. For example, the digester may be part of amunicipal wastewater treatment plant or an agricultural or industrialdigester. Methane production in the digester increases. The syngas maybe added to the digester without pretreatment other than lowering itstemperature.

An apparatus and process are described herein for transferring syngas todigestate. A jet ejector pump is used to aspirate into a stream ofdigestate flowing in a pipe. The digestate may be flowing in a dedicatedrecirculation loop. A pump generates a primary flow. An ejector nozzleat the pump discharge draws and mixes a secondary flow of syngas intothe primary flow. The liquid and gas are combined into a liquid jetcontaining fine syngas bubbles. This mixture exits in one or morelocations in a digester tank.

Optionally, the pumped jet aspiration system may also provide mixing forthe digester. In another option, gas from the headspace of the digestercan be mixed into digestate to encourage further conversion of CO and H₂in the syngas or biogas to methane. In another option, heat from syngasleaving a pyrolysis reactor may be recovered and used, for example, forpartial drying of the digestate.

Optionally, a condensable portion of the syngas may be condensed, forexample by indirect condensing, and fed to the digester as a liquid. Aremaining gas portion of the syngas is fed to the digester as describedabove.

In a process and apparatus for treating wastewater, such as municipalsewage, a digestate cake is further thermally dried and then fed to apyrolysis system to produce syngas and char. The syngas is preferablycooled to recover its heat for cake drying, and then introduced into oneor more anaerobic digesters for bioconversion of syngas into methane.The methane may be used as a fuel for heat or generating electricity.The biochar resulting from the pyrolysis process may be used as soilenhancer.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 is a schematic process flow diagram of an anaerobic digestion andpyrolysis system.

DETAILED DESCRIPTION

In this specification, the term pyrolysis includes pyrolysis,gasification, and related methods involving heating biomass withoutsufficient oxygen to support combustion. The term syngas includes,unless stated otherwise, vapors such as vaporized pyrolysis oil, watervapor, and vapors of pyroligneous acid. The word digestate is sometimesused to refer to only the solids fraction of the sludge produced by ananaerobic digester but in this specification digestate typically refersto the whole digester sludge.

There is experimental evidence that syngas can be converted throughanaerobic digestion to biogas containing mainly methane. CO in thesyngas is used as a substrate or food for certain strains ofmethanogenic archea in direct reactions that include hydrogen and waterto produce methane. Other indirect reactions also occur, wherein CO andH₂ are converted to acetate or methanol and finally to methane byanaerobic bacteria. Regardless of the specific reaction, the methaneyield is 0.25 mol of CH₄ per mol of CO, plus 0.25 mol of CH₄ per mol ofH₂. Based on the range of CO and H₂ typically contained in syngas, thisis equivalent to about 0.2 to 0.4 standard m³ of methane production perkilogram of VS gasified, when the syngas is efficiently introduced anddissolved in the anaerobic mixed liquor. The range in syngas compositionis a function of the type of biomass gasified and the conditions of thepyrolysis process.

The solids in dewatered digestate cake have a lower energy content thanthe undigested raw solids in the digester feedstock because a portion ofthe carbon contained in the VS was converted by digester anaerobicbacteria into methane and carbon dioxide. In the case where acombination of primary and secondary municipal sewage sludge (forexample from an activated sludge sewage plant) is fed to a digester, theenergy content of undigested solids with a 70% VS content may be about7000 Btu per pound of dry solids (DS). In anaerobic digester sludge witha 48% VS content, the energy value may be 4800 Btu/ lb DS depending onthe degree of VS reduction. Depending on the VS content of the rawmunicipal sewage sludge, its heat content can be as high as 7400 Btu/lbDS, and the heat content of the anaerobic digester sludge may be as highas 5700 Btu/lb DS. The digestate produced from feedstocks with higherfiber content tends to have a higher heat value.

The energy value of the digestate solids can be extracted by pyrolysisor oxidation of the dewatered cake. Depending on the heat content of thedigestate solids, further thermal drying after mechanical dewatering maybe required to be able to support auto-thermal pyrolysis of thedigestate to produce syngas without the need to introduce additionalexternal heat to support pyrolysis. The solids content required tosupport auto-thermal pyrolysis may range from 40% to 70% or higher.Depending on the type of pyrolysis equipment, required solids content ofthe feed may be as high as 90%.

The cake can be dried using direct or indirect dryers. Direct beltdryers are more versatile as they enable the use of low temperature heatsources such as heat recovered from engine generators, condensate, etc.

The syngas is introduced into a digester for the purpose of producingmethane. The syngas can come from one or more of any form of gasifiedraw biomass such as wood, municipal solids waste, municipal yard waste(for example grass clippings, leaves or plant clippings), primary orwaste activated sludge from a wastewater treatment plant such as amunicipal sewage plant, agricultural residues, etc.; or frompyrolysis/gasification of dewatered and partially dried digestate cakeproduced by the same or other digester at the same or other digestionfacility. The facility can be a municipal wastewater treatment plant oran agricultural or industrial digester. Methane production in thedigester increases as it results from two sources, the fermentation ofVS in the feedstock and the bioconversion of the syngas (CO and H₂) tomethane. Syngas does not require pretreatment for introduction into thedigester, only lowering its temperature. In cases where the pyrolysisfeedstock includes lignocellulosic material, pyrolysis allows carbon inthe lignocellulosic material to be consumed in the digester.

The solubility of CO and H₂ in water is low, therefore syngas biologicalconversion to methane is limited by the gas-liquid mass transfer. Toincrease the gas liquid mass transfer rate, the syngas is preferablyadded to the digestate in small bubbles, for example of 1000 microns orless in diameter, or by transfer across a gas permeable membrane.

A jet ejector pump or aspirator may be used to aspirate syngas. Thesyngas may be cooled and stored in a gas holder. A pump recirculatessludge from the digester. This pump can be, for example, a chopper pumpor an open impeller end suction centrifugal pump. The pump generates aprimary flow. An ejector nozzle at the pump discharge reduces the pipediameter and accelerates the sludge flow, lowering the pressure. Thisresults in a secondary flow of syngas from the gas holder being drawninto the ejector. The turbulence in the ejector nozzle causes an activemixing zone where the liquid and gas are combined into a liquid jetcontaining fine syngas bubbles. The mixture exits in one or morelocations around the lower third of the digester tank where jet nozzlesare placed. This increases the mass transfer between gas and liquid andenables the syngas to dissolve in the digestate. Further, if the gasincludes vapors, contact with the liquid condenses the vapors whileheating the liquid.

An alternative method to create syngas microbubbles is to use amicrobubble generator pump, such as made by Honda Pumps. These pumps areused for dissolved air flotation or ozone injection and create gasmicrobubbles of 50 micron diameter or less, which may be an order ofmagnitude smaller than bubbles produced by many gas eductors oraspirators. The microbubbles are dispersed in recirculating digestate orfiltrate flow by connecting the pump gas inlet to the syngas storageholder. With smaller bubbles, the gas/water interface surface area isincreased, gas holdup time in the water column also increases, anddigester foaming is reduced.

The syngas may include one or more condensable gasses. In that cases,the condensable gasses may be introduced into the digester as a gas asdescribed above. Alternatively, at least some of the condensable gas maybe condensed and introduced into the digester as a liquid. For example,the syngas may go through an indirect condensing step before remaininggas is fed to the digester.

In digesters with high solids content and fibers in the digestate, ascrew press or other solids separator can be used to produce a filtratethat is more suitable for receiving syngas bubbles. The recirculatingdigestate or filtrate stream is used primarily for gas/liquid masstransfer but may also serve the purpose of total or partial mixing,particularly in digesters operated with low solids content (2 to 4%). Indigesters with higher solids content further mechanical mixing is likelyto be required. However, mixing may bring syngas bubbles to the surfaceof the digester before they have a chance to dissolve into thedigestate. Many digesters are mixed intermittently, for example ¼ to ⅓of the time. Optionally, microbubbles or larger ejector or aspirator gasbubbles may be fed only during non-mixing periods to reduceshort-circuiting of bubbles to the surface aided by vertical mechanicalmixing energy.

When implemented in a high solids digester such as a two stage Triton™digester from UTS or Anaergia, sludge from the second stage may be usedfor recirculation and gas entrainment, as the solids content is lowerand so is the viscosity. Syngas reintroduction is preferably done in thesecond stage of high solids two stage digesters. The syngas injectionprocess can be used with mesophilic or thermophilic digesters, but theconversion efficiency of syngas to methane is higher under thermophilicconditions.

An intake to the aspirator nozzle can also be connected to the headspaceof the digester, such that the nozzle aspirates a combination of biogasand syngas. The relative flow of the gasses is regulated with valves inone or both gas supply lines. If the quality of the biogas collected inthe headspace of the digester decreases (increased CO and H₂ content)materially as a result off syngas introduction into the digester liquid,this is an indication of incomplete syngas conversion to methane. Biogasfrom the headspace can be reintroduced into the digester liquid so thatCO and H₂ in the headspace gas are converted to methane.

Syngas will exit the pyrolysis reactor at 250 degrees C. or more, or 400or 500 to 700 deg C. or more. The syngas is cooled for introduction intothe digester. A gas/liquid heat exchanger can be used to recover heatfrom the syngas. The heat recovered as hot water can be used for partialdrying of the cake in a low temperature direct belt dryer. Anotheroption to recover heat from the syngas for cake drying is to use agas/gas heat exchanger wherein syngas heat is transferred to air used inthe belt dryer.

Preferably, the temperature and residence time of the pyrolysis reactorare sufficient to produce syngas wherein components other than watervapor are primarily carbon monoxide or hydrogen. However, there may alsobe other condensable gasses or liquid droplets in the syngas of othercompounds such as oils, waxes or other organics, collectively called“oils” or “organics”. A syngas condenser, downsteam of or integratedwith the gas heat exchanger, condenses the syngas to allow the watervapor and oils to be removed as a liquid fraction of the syngas from agas fraction of the syngas. The syngas condenser may be, for example, adirect condenser having a recirculated cooled syngas liquid fractionwithin a contact chamber or an indirect condenser.

The gas fraction of the syngas flows to a gas holder and eventually tothe anaerobic digester. The liquid fraction of the syngas optionallyflows to an oil-water separator, for example a centrifuge, to create awater fraction and an organics fraction. The water fraction may bedischarged for further treatment, optionally to the anaerobic digesterif discharge to a sewer is not permitted and no other treatment meansare located nearby. The water fraction contains some residual organicsand so operates as a bleed preventing the accumulation of recalcitrantcompounds.

The organics fraction of the liquid fraction of the syngas may be sentto the digester but it is preferably returned to the pyrolysis reactor.In the pyrolysis reactor, at least a portion of the returned organicsare converted to carbon monoxide and hydrogen or other gaseouscomponents of the syngas. This effectively increases the residence timefor compounds requiring additional time to be converted into gasses.

Digested sludge disposal in municipal wastewater treatment plants is agrowing concern due to rising costs and limitations in the ability toapply the sludge to land. The pyrolysis process results in syngas andchar. Char, also called bio-char, contains carbon and ash. Ash is thenon-volatile or inert, solids present in the sludge. Some of thesesolids are nutrients such as phosphorous and potassium or otherminerals. Char is a sanitized product as a result of the hightemperature process that produces it. The char volume is a fraction ofthat of the sludge cake, and can be used as soil enhancer. Biochar canbe used for one or more purposes such as a soil amendment to improvecrop yield, to support crops that require high potash and elevated pH,to improve water quality, to reduce soil emissions of greenhouse gases,to reduce nutrient leaching, to reduce soil acidity, and to reduceirrigation and fertilizer requirements. These positive qualities aredependent on the properties of the biochar, and may depend on regionalconditions including soil type, soil conditions, temperature, andhumidity. In some cases, modest additions of biochar to soil may reducenitrous oxide (N₂O) emissions by up to 80% and essentially eliminatemethane emissions. N₂O and methane are both more potent greenhouse gasesthan CO₂. Biochar can store greenhouse gases in the ground thuspotentially helping to reduce or stall the growth in atmosphericgreenhouse gas levels. Biochar can sequester carbon in the soil forhundreds to thousands of years, like coal.

In one application, a municipal wastewater treatment plant or processsuch as an activated sludge plant is coupled with an anaerobic digester.Primary and waste activated (secondary) sludge from the wastewatertreatment plant is sent to the digester. The digester produces digestatewhich is de-watered to produce a cake. The digester sludge cake isfurther thermally dried and then fed to a pyrolysis system to producesyngas and char. The syngas is cooled, preferably while recovering itsheat for example for cake drying. The cooled syngas is introduced intoone or more digesters, for example the digester that produced thedigestate, for bioconversion of syngas CO and H₂ into methane, mediatedby bacteria and archea present in the digester bacterial consortium thatalso ferments the volatile solids fed to the digester in the raw primaryand secondary sludge. Optionally, primary and secondary sludge may befed first to the pyrolysis system rather than being fed to the digesterdirectly. The methane produced by the two processes in the digestercombine in the digester headspace and may be used for energy generationwith engines, turbines or fuel cells, or upgraded to biomethane forinjection into the natural gas grid. The biochar resulting from thepyrolysis process may be used as soil enhancer. Compared to a system inwhich a digester merely treated sludge from the wastewater treatmentplant, there may be less waste produced or the net energy consumptionmay be reduced, or both, per unit of sewage treated.

Bio-char from gasification of digested municipal sludge or a digestatefrom an agricultural or industrial digesters can be used as a soilenhancer or a source of nutrients, mainly phosphorous and potassium.

In an example shown in FIG. 1, an anaerobic digester 1, alternativelyreferred to as a digester for brevity, is combined with a system forpyrolysing its digestate B. The digester 1 is fed with a feedstock Awhich may comprise one or more of: a sludge, for example primary orwaste activated sludge or both from a wastewater treatment plant such asa municipal sewage plant; municipal solid waste; municipal yard waste;an industrial waste; or, an agricultural waste. The digester 1 producesproduct biogas O which may, for example, be used to produce energy orupgraded to produce biomethane.

The digester 1 may have one or more mixed covered tanks. Suitabledigesters are sold under the Triton™ and Helios™ trade marks by UTS orAnaergia. Digestate B flows from the digester 1 to a mechanicaldewatering unit 3, for example a centrifuge, filter press or screwpress. The mechanical dewatering unit 3 separates the digestate B into aliquid fraction F and a de-watered digestate cake E. The liquid portionF of the digestate B, in some cases called a filtrate or centrate, maybe discharged or re-used, optionally after further treatment.Optionally, the digester 1 may be located near a municipal sewagetreatment plant and the liquid portion F may be returned to themunicipal sewage treatment plant for further treatment. In this case,the digester preferably treats primary and waste activated (secondary)sludge from the sewage treatment plant either as some or all of thedigester feedstock A or as some or all of an optional external biomassfor gasification M.

The de-watered digestate cake E is sent to an optional sludge cake dryer4 if required, or beneficial, to reduce the water content of the cake Ebefore pyrolysis. Hot air and moisture H produced by the dryer 4 may besent to a heat recovery treatment unit to extract waste heat for reuse,for example to help heat the digester 1, the pyrolysis reactor 5 or thedryer 4. The hot air and moisture H may also be treated, for example toreduce ordors, before it is discharged.

The sludge cake dryer 4 produces a partially dried cake G. Some or allof the partially dried cake G which is sent to a pyrolysis reactor 5.Optionally, the pyrolysis reactor 5 may be fed with external biomass Mfor pyrolysis. The external biomass M may be any one or more of thematerials described for the digester feedstock 1. However, the externalbiomass M is treated by pyrolysis before it enters the digester 1.

The pyrolysis reactor heats its one or more feed materials, for exampleto between 400 or 500 and 700 degrees C., or alternatively between 175and 400 degrees C., in the absence or a deficiency of oxygen, to producebiochar J and hot syngas I. Optionally, biochar J may be used as a soilenhancer typically after being collected and stored temporarily and thenhauled off site. Hot syngas I is preferably sent to a gas heat exchanger6 to produce a cooled syngas K and recovered heat L. Recovered heat Lmay be re-used in the system or elsewhere. For example, recovered heat Lmay be used to help heat the digester 1, the pyrolysis reactor 5 or thesludge dryer 4.

Cooled syngas K is optionally sent to a syngas condenser 8. The syngascondenser 8 separates the cooled syngas K into a gas fraction P and aliquid fraction Q. The syngas condenser 8 does not necessarily condenseall condensable gasses in the cooled syngas K. The liquid fraction Q maybe sent to the digester 1. However, the liquid fraction Q is preferablysent to an oil-water separator 9 to produce a water fraction R and anorganic fraction S. The water fraction R may contain some organiccompounds and may be treated further before it is discharged or-used.The organic fraction S may include water but contains a higherconcentration of organic compounds than the liquid fraction Q. Theorganic fraction S may be treated or upgraded to produce usableproducts. Alternatively, the organic fraction S is returned to thepyrolysis reactor 5. In this alternative, in the absence of a practicalor economical way to make a higher value use of the organic fraction S,the amount of gas fraction P sent to the digester 1 can be increased,which is typically preferable to sending the organic fraction S, orcondensable or condensed gases, to the digester 1.

Optionally, the gas fraction P may be collected and stored in a gasholder 7. The gas fraction P may also optionally be mixed with digesterbiogas N. With or without digester biogas N, the gas fraction P is sentto a pumped gas aspirator 2. Optionally, the gas aspirator 2 may bereplaced by another microbubble generator or a gas transfer membrane.recirculating digestate C is withdrawn from the digester 1, typically byway of a pump, and passes through the aspirator 2. Digestate withblended syngas D returns to the digester 1. In this way, the gasfraction P is added to digestate in the digester 1.

Other alternative systems and methods may be devised within the scope ofthe following claims.

The components and streams in FIG. 1 are listed below, in some caseswith additional description.

-   1. Anaerobic digester-   2. Pumped gas aspirator-   3. Mechanical dewatering unit-   4. Sludge cake dryer-   5. Pyrolysis reactor-   6. Gas heat exchanger-   7. Gas holder (for cooled syngas)-   8. Syngas condenser-   9. Oil-water separator-   A. Digester feedstock-   B. Digestate (to dewatering)-   C. Recirculating digestate-   D. Digestate with blended syngas-   E. Dewatered digestate cake-   F. Liquid portion (ie. filtrate or centrate) from dewatering,    optionally sent to plant headworks or further treatment-   G. Partially dried cake (to pyrolysis reactor)-   H. Hot air and moisture from dryer, optionally to heat recovery or    treatment or both-   I. Hot syngas-   J. Biochar, optionally to storage or hauling for use as soil    enhancer-   K. Cooled syngas-   L. Recovered heat (from syngas, optionally to cake dryer)-   M. External biomass (for pyrolysis)-   N. Digester biogas, returning for injection into digester liquid-   O. Product biogas, optionally to utilization for energy production    or upgrading to biomethane-   P. Gas fraction (of syngas)-   Q. Liquid fraction (of syngas)-   R. Water fraction (of liquid fraction of syngas)-   S. Organic fraction (of liquid fraction of syngas)

We claim:
 1. A process comprising steps of, a) producing a synthesis gasfrom pyrolysis of a feedstock; and, b) adding the synthesis gas to ananaerobic digester.
 2. The process of claim 1 wherein the feedstockcomprises one or more of a raw biomass, wood, municipal yard waste,municipal solids waste, primary sludge from a wastewater treatmentplant, waste activated sludge from a wastewater treatment plant or anagricultural waste or residue.
 3. The process of claim 1 wherein thefeedstock comprises digestate.
 4. The process of claim 3 wherein thedigestate is produced by the anaerobic digester.
 5. The process of claim1 wherein the anaerobic digester is coupled with or part of a municipalwastewater treatment plant, or an agricultural or industrial digester.6. The process of claim 1 wherein the synthesis gas is cooled before itis fed to the digester.
 7. The process of claim 1 wherein condensableorganic compounds are removed from the synthesis gas and returned asfeedstock to step a).
 8. An apparatus for transferring syngas todigestate comprising, a) a pipe between a source of digestate and adigester; b) a pump to create a flow of digestate in the pipe; c) anejector, microbubble pump or gas transfer membrane in communication withpipe having an inlet connected to a source of the syngas.
 9. Theapparatus of claim 8 wherein the source of digestate is the digester.10. The apparatus of claim 8 wherein the pipe is connected to multipleoutlets in the digester.
 11. The apparatus of claim 8 wherein the inletis further connected to the headspace of the digester.
 12. The apparatusof claim 8 further comprising a heat exchanger between the ejector andthe source of the syngas.
 13. The apparatus of claim 12 wherein the heatexchange provides heat to a digestate cake drier.
 14. A process andapparatus for treating wastewater comprising, a) treating the wastewaterto generate a sludge; b) feeding the sludge to an anaerobic digester toproduce biogas and digestate; c) dewatering the digestate to produce acake; d) thermally drying the cake to produce a dried cake; e)pyrolysing the dried cake to produce char and syngas; f) feeding thesyngas to the anaerobic digester.
 15. The process of claim 14 furthercomprising extracting heat from the syngas and using the extracted heatin step d).
 16. The process of claim 14 comprising using the char as asoil enhancer.
 17. The process of claim 14 comprising steps ofextracting a condensable gas from the syngas, pyrolysing the condensablegas to produce additional syngas, and feeding the additional syngas tothe digester.
 18. The process of claim 14 wherein step e) is conductedat a temperature of 250 degrees C. or more.
 19. The process of claim 14wherein the syngas includes one or more vapors and step f) comprisescondensing the one or more vapors on contact with a digestate from theanaerobic digester.